WO2010112431A1 - Age-resistant catalyst for oxidation of no to no2 in exhaust streams - Google Patents

Abstract

The present invention relates to a zeolite comprising platinum. The invention furthermore relates to a method for producing said zeolite comprising platinum according to the invention, to the use of said zeolite as an oxidation catalyst and hydrocarbon reservoir and to a catalyst component comprising the zeolite according to the invention.

Description

Aging stable catalyst for the oxidation of NO to NO ₂ in

waste gas streams

The present invention relates to a platinum-containing zeolite. The invention further relates to a process for the preparation of platinum-containing zeolites according to the invention, the use of the zeolite as

Oxidation catalyst and hydrocarbon storage and a catalyst component containing the zeolite of the invention.

At the beginning of the exhaust gas purification of internal combustion engines, only the exhaust gases of gasoline engines with three-way catalysts (TWC) were cleaned. The nitrogen oxides are reduced with the reducing hydrocarbons (HC) and carbon monoxide (CO).

For about 15 years, attempts have also been made to treat the exhaust gases from diesel engines with catalytic converters. The exhaust of diesel engines includes carbon monoxide, unburned hydrocarbons, nitrogen oxides and soot particles

Air pollutants on. The unburned hydrocarbons include paraffins, olefins, aldehydes and aromatics.

An exhaust system for diesel internal combustion engines usually consists of the following components:

• Diesel Oxidation Catalyst (DOC) for the oxidation of

Hydrocarbons and as hydrocarbon storage in cold start; • Diesel Particulate Filter (DPF) to reduce particulate emissions;

• optionally a hydrolysis catalyst for

Urea decomposition; • SCR catalytic converter (selective catalytic reduction) for the reduction of nitrogen oxides;

• Blocking catalyst as ammonia oxidation catalyst.

Under DOC (Diesel Oxidation Catalyst) the skilled person understands a catalyst which preferably performs a hydrocarbon storage function in the cold start and oxidizes unburned hydrocarbons in normal operation. The treatment of the exhaust gases of diesel engines with catalytic converters requires conceptual changes to the catalyst materials, since a diesel engine is always operated in excess of oxygen, unlike a gasoline engine and thus the catalyst is never exposed to reductive conditions.

Since the emergence of the discussion about the problem of particulate matter, the DOC catalysts are still followed by particle filters. Particulate filters (DPF, diesel particulate filters) are used to filter soot particles from the exhaust gas of internal combustion engines, especially diesel engines, and thus to reduce their emission into the atmosphere. Here are various filter concepts, such. However, the real difficulty is not in the filtration of the soot particles, but in the regeneration of the filters used carbon carbon burns spontaneously depending on the operational composition of the particles only at temperatures between 500 ⁰ C and 700 ⁰ C. Particle filters of the newer generation must be actively regenerated. This means that it is necessary to repeatedly generate such a high temperature on the DOC that the soot on the downstream DPF ignites and burns off. Therefore, the thermal aging of the DOC catalysts plays an important role today.

Newer generation diesel vehicles are currently equipped with a unit downstream of the diesel particulate filter that can accomplish a selective catalytic reduction of nitrogen oxides using a so-called SCR catalyst. Selective catalytic reduction (SCR) refers to the selective catalytic reduction of nitrogen oxides from exhaust gases of combustion engines and also power plants. With an SCR catalyst, only the

Nitrogen oxides NO and NO ₂ (commonly referred to as NO _x ) selectively reduced, wherein for the reaction usually NH ₃ (ammonia) is mixed. Therefore, only the harmless substances water and nitrogen are formed as reaction products.

Of particular importance today is, in addition to the oxidation of hydrocarbons, the oxidation of NO to NO ₂ in the diesel oxidation catalyst. The NO ₂ facilitates regeneration of the subsequent diesel particulate filter, ie, soot burn-off (see, for example, J. Choo et al., Science of the total environment (2008) 396-401, M. Jeguirim et al., Applied Catalysis B: Environmental, 76 (2007) ), 235-240 or K. Yamamoto et al., Proceedings of the Combustion Institute, article in press). In addition, a mixture of NO / NO _{2 can be} faster by selective catalytic reduction (SCR) with

Ammonia to nitrogen and air are decomposed to be pure NO (see, for example, A. Grossale, et al., Journal of Catalysis, 256 (2008), 312-322, or M. Schwidder, et al., Journal of Catalysis, 259 (2008) , 96 to 103), so here the activity of the DOC for the oxidation of NO to NO ₂ must be very high even after aging of the catalyst.

Thus, catalysts are required which have a lower tendency to age under the operating conditions of the diesel exhaust aftertreatment than has hitherto been possible in the prior art.

In addition to Pt-based catalysts, catalysts which contain both Pt and Pd are known in the prior art. Furthermore, DOC catalysts often contain zeolites, which serve to store the hydrocarbons in the cold state (cold start trap), so that the cold start emissions of hydrocarbons are reduced.

A typical DOC is disclosed, for example, in EP 800 856 A2. It contains with 3 to 4 g Pt / 1 catalyst volume a high noble metal concentration. However, to achieve the lowest possible light-off temperature for CO and hydrocarbon, most of the platinum is deposited on an amorphous Al / Si mixed oxide and only a small portion on the zeolite. According to the prior art, it has hitherto not been possible to distribute a very high platinum concentration so homogeneously in the zeolite that it still has a good platinum dispersion even after a higher temperature load. The high platinum amount or dispersion causes sufficient stability, which is why in the prior art, the high amount of platinum was introduced into an Al / Si mixed oxide and not in the zeolites.

Platinum-containing zeolites are known in the art. For example, zeolites with very low platinum contents (<1%) are used as catalysts in the refinery sector, for example for cyclization, aromatization, and Cracking reactions. In contrast to the conditions prevailing in a diesel exhaust, the reactions just mentioned take place under reductive conditions (ie excess of hydrocarbons) and therefore require only very low precious metal contents.

The preparation of platinum-containing zeolites, for example by ion exchange of platinum in the pores of the zeolite, is known in the art. However, these processes did not result in platinum concentrations in the zeolite that would be necessary for use in a diesel oxidation catalyst (see, for example, JM Garcia-Cortes et al., Journal of Catalysis, 218 (2003), 111-122; C. Jimenez et al. Applied Catalysis A: General 249 (2003), 175-185 and J. Perez-

Ramirez et al., Applied Catalysis B: Environmental 29 (2001), 285-298).

DOC catalysts with improved stability are also commonly provided by mixed Pt / Pd catalysts. In particular, Pt / Pd catalysts with a high Pt content (6: 1) show good thermal aging stability. The disadvantage, however, is that the NO to NO ₂ - oxidation is worse with increasing Pd contents. In addition, the Pt / Pd catalysts are significantly less resistant to sulfur (see, for example, 5th International Forum on Exhaust and Particle Emissions, 19 and 20 February 2008, Ludwigsburg, pages 126 to 144). Such catalysts usually can not be thermally regenerated after sulfur poisoning but continue to lose

Activity if they are thermally stressed after poisoning, ie aged. The object of the present invention was therefore to provide a process for the preparation of a catalyst, in particular a diesel oxidation catalyst, which has a low tendency to age and high activity.

The object is achieved by a method for producing a platinum-containing zeolite comprising the steps

a) impregnating a zeolite with a platinum sulphite solution, b) calcining the impregnated zeolite under a protective gas atmosphere.

The calcination should preferably be carried out in a protective gas atmosphere, preferably an argon atmosphere,

Nitrogen atmosphere or other inert atmosphere is used. Particularly preferred is an argon atmosphere.

The calcination of the impregnated zeolite is preferably carried out at a temperature of 600 to 900 ⁰ C, more preferably> 750 to 850 ⁰ C, more preferably> 750 to 830 ⁰ C, in particular at about 800 ⁰ C.

Calcining produces a platinum precursor compound which, if necessary, is preferably reduced following calcination. In principle, however, a reduction can already take place during the calcination, in which case, however, a reducing atmosphere would have to be used instead of the inert gas atmosphere.

A reduction which can be carried out after calcination is preferably carried out from a mixture of a reducing gas (hydrogen, carbon monoxide, ethene, a methanol, ethanol, etc.) and an inert gas. Preferred inert gases are, for example, argon, helium, neon and the like. The inert gas in the reduction step is to be understood as carrier gas, hydrogen or another reductive gas preferably being present in a concentration of 1 to 10% by volume, more preferably 3 to 7% by volume, particularly preferably about 5% by volume, based on the total volume of reducing gas and inert gas amounts.

The reduction is usually carried out until a complete or almost complete implementation of the

Platinum lead connection is done. The reduction is preferably carried out over a period of 3 to 7 hours, more preferably 4 to 6 hours, particularly preferably about 5 hours.

The reduction is preferably carried out at elevated temperatures. Preferably, the reduction is carried out at a temperature of from 200 to 500 ^° C, more preferably from 250 to 350 ^° C, most preferably about 300 ^° C. For the reduction, the catalyst is usually in a

Catalyst bed given while flowing through the reducing agent. Likewise, the catalyst can be coated with the reducing gas and advantageously brought to an elevated temperature. The increase in the temperature can be effected, for example, by heating the catalyst bed. It is also possible that the Reduktionsgsgas is already heated in advance, for example by the gas inlet is heated, in which case the heated reducing gas is passed over the catalyst to be reduced.

Impregnation of the zeolite with the platinum sulphite solution can be carried out by dip impregnation, spray impregnation or incipient wetness method. Preferably, the Impregnation via an incipient wetness method, although according to the prior art usually in this impregnation method only a small part of the metal clusters migrate into the pores and a considerable part remains on the outer zeolite surface.

Surprisingly, however, it has been found that incipient wetness impregnation of the zeolite powder with platinum sulphite acid (PSA) and subsequent calcination under protective gas at high temperatures produce a catalyst which still has the largest part of the platinum in the zeolite pores even after this high temperature load. This can be demonstrated by an X-ray diffractogram (XRD) and by CO adsorption (after selective poisoning of the Pt clusters on the surface) in the FTIR. XRD and FTIR are standard analytical methods in chemistry.

Surprisingly, it was also found that the catalyst thus prepared has an increased sulfur resistance than already known systems. The catalytic activity of the thermally aged catalyst according to the invention is not changed by sulfur poisoning and subsequent high-temperature desulfurization.

Although the catalyst developed shows a comparable aging behavior with respect to the oxidation of carbon monoxide as existing Pt-based catalysts, it has surprisingly been found that it has a significantly better stability with regard to the oxidation of NO.

A further advantage of the catalyst according to the invention over the prior art is that the precious metal can only be reduced to one component, the zeolite, is applied, and not, as with other catalysts on a mixture of zeolite and additional oxidic carriers. As a result, manufacturing steps and thus costs can be saved.

The increased zeolite content also significantly increases the storage capacity for hydrocarbons (see, for example, EP 691 883 B1, US Pat. No. 5,804,155 and EP 830 301). The storage capacity is of great importance if the catalytic converter has not yet reached the required operating temperature and the resulting exhaust gases can not yet burn.

The invention thus also relates to a zeolite which is produced in particular by the process according to the invention.

The term "zeolite" in the context of the present invention as defined by the International Mineralical Association (D.S. Coombs et al., Canadian Mineralogist, 35, 1979, 1571) is a crystalline substance from the group of aluminum silicates having a network structure of the general formula

M _{x / n} [(AlO ₂ ) _x (SiO ₂ ) _y ] x (H ₂ O) ₂

understood that consist of SiO ₄ / AlO ₄ tetrahedra, which are linked by common oxygen atoms to a regular three-dimensional network.

The ratio of Si / Al = y / x is always> 1 according to the so-called "Lowenstein rule", which prohibits the adjacent occurrence of two adjacent negatively charged A10 ₄ tetrahedra, although there are more at a lower Si / Al ratio Replacement places are available for metal, but the zeolite becomes increasingly thermally unstable. The zeolite structure contains voids, channels that are characteristic of each zeolite. The zeolites are classified into different structures according to their topology. The zeolite skeleton contains open cavities in the form of channels and cages which are normally occupied by water molecules and additional skeletal cations which can be exchanged. An aluminum atom has an excess negative charge which is compensated by these cations. The interior of the pore system represents the catalytically active surface. The more aluminum and the less silicon a zeolite contains, the denser the negative charge in its lattice and the more polar its inner surface. The pore size and structure is determined by the Si / Al ratio (modulus), which accounts for most of the catalytic character of a catalyst, in addition to parameters of preparation, ie, use or type of template, pH, pressure, temperature, presence of seed crystals Make up zeolites.

Preferably, the zeolite of the present invention contains at least 2 weight percent platinum, preferably at least 3 weight percent, most preferably 3.5 or more weight percent platinum with at least 90 percent of the platinum in the pores of the zeolite, more preferably at least 95%, particularly preferably at least 99%.

Preferably, the zeolite is selected from the groups consisting of the types AEL, BEA, CHA, EUO, FAU, FER, KFI, LTA, LTL, MAZ, MOR, MEL, MTW, LEV, OFF, TON, and MFI. Particularly preferred is the BEA structure.

Preferably, the zeolite has a SiO ₂ / Al ₂ O ₃ modulus of from 5 to 300, more preferably from 10 to 200, most preferably from 15 to 100. The zeolite according to the invention is characterized by a Pt-C =O stretching vibration between 2070 and 2110 cm ^-1 , preferably at about 2080 to 2095 cm ^-1 . The stretching vibration is present even after poisoning with adamantanecarbonitrile. Adamantancarbonitrile is a sterically demanding molecule that due to its size can not penetrate into the pore system of the zeolite. Due to the adsorption of adamantanecarbonitrile only Pt clusters on the outer surface of the poisoned. If CO is adsorbed following this poisoning, it can only bind to the non-poisoned Pt clusters in the interior of the zeolite. The presence of the Pt-C = O stretching vibration after poisoning with adamantanecarbonitrile proves that the Pt sits in the pores of the zeolite. The remaining intensity after poisoning is about 2- to 4-fold higher than in a comparative catalyst.

The inventive zeolite is also in

X-ray diffractogram (XRD) free from Pt reflections. This also shows that the platinum sits in the pores of the zeolite.

Another object of the invention is the use of the novel zeolites as oxidation catalyst and hydrocarbon storage. Zeolites are as

Hydrocarbon storage known. In connection with the high platinum dispersion in the pores of the zeolite, however, it is also outstandingly suitable as an oxidation catalyst with a corresponding cumulative hydrocarbon storage function. The fact that platinum is applied only to a zeolite and not, as known in the art, to other metal oxides, results in a simple catalyst system that can be produced inexpensively. The zeolite according to the invention can advantageously be processed into a washcoat and applied correspondingly to a catalyst carrier body. How such a washcoat can be made is known to the person skilled in the art. The necessary coating techniques for coating a catalyst carrier body are also known to the person skilled in the art. For example, the impregnated and dried zeolite is processed into an aqueous coating dispersion. A binder, for example silica sol, may be added to this dispersion. The viscosity of the dispersion can be adjusted by its own additives, so that it is possible to apply the required amount of coating in a single operation on the walls of the flow channels. If this is not possible, then the coating can be repeated several times, wherein the freshly applied coating is fixed in each case by an intermediate drying and calcined as needed.

For the exhaust gas purification of diesel engines coating amounts of 50 to 500 g / l, preferably 250 to 350 g / l volume of the catalyst carrier body are advantageous.

Another object of the invention is a catalyst component containing a zeolite according to the invention. It is preferred that the zeolite is present as a coating on the carrier.

As a catalyst support, a metallic or ceramic monolith, a nonwoven or a metal foam may be used. Other known in the art

Catalyst shaped bodies or catalyst carrier bodies are suitable according to the invention. Particularly preferred is a metallic or ceramic monolith having a plurality of parallel passage openings, which with the Washcoat coating be provided. The carrier body preferably has passage openings with a round, triangular, quadrangular or polygonal cross section. Particularly preferably, the carrier is designed as a monolithic honeycomb body.

Metallic honeycomb bodies are often formed from metal sheets or metal foils. In this case, the honeycomb bodies are produced, for example, by alternating arrangement of layers of structured sheets or films. Preferably, these arrangements consist of a position of a smooth sheet alternating with a corrugated sheet, wherein the corrugation may be formed, for example, sinusoidal, trapezoidal, omega-shaped or zigzag. Corresponding metallic honeycomb bodies and processes for their preparation are described, for example, in EP 0 049 489 A1 or DE 28 56 030 A1.

In the area of the catalyst carrier bodies, metallic honeycomb bodies have the advantage that they heat up more quickly and thus generally show better catalyst response on the basis of metallic substrates in cold start conditions.

The honeycomb body preferably has a cell density of 30 to 1500 cpsi, particularly preferably 200 to 600 cpsi, in particular about 400 cpsi.

The Katalysatortragerkorper, on which the inventive catalyst may be applied, may be formed of any metal or a metal alloy and z. B. by extrusion or by winding or stacking or folding of metal foils. Known in the field of emission control are temperature-resistant alloys with the Main components iron, chromium and aluminum. Preferred for the catalyst according to the invention are freely permeable monolithic catalyst carrier bodies with or without inner leading edges for the turbulence of the exhaust gas or metal foams which have a large inner surface and to which the catalyst according to the invention adheres very well. However, catalyst carrier bodies with slots, perforations, perforations and embossments can also be used in the metal foil.

In the same way, catalyst carrier bodies made of ceramic material can be used. Preferably, the ceramic material is an inert, low surface area material such as cordierite, mullite, aluminum titanate or α-alumina. However, the catalyst support used may also consist of high surface area support material such as γ-alumina.

Likewise, a metal foam, for example a metallic open-pore foam material, can be used as the catalyst carrier body. In the context of the present invention, the term "metallic open-pore foam material" is to be understood as meaning a foam material made of any desired metal or alloy, which may optionally also contain additives and which has a multiplicity of pores which are conductively connected to one another such that For example, a gas can be passed through the foam material.

Metallic open cell foam materials have a very low density due to the pores and voids, but have considerable rigidity and strength. The production of metal foams, for example, by means of a metal powder and a metal hydride. Both powders are usually mixed together and then through Hot pressing or extrusion to a molding material compacted. The molding material is then heated to a temperature above the melting point of the metals. The metal hydride releases hydrogen gas and foams the mixture.

However, there are other ways to make metal foam, for example, by blowing gas into a molten metal, which was made foamable beforehand by adding solid components. For aluminum alloys, for example, 10 to 20% by volume of silicon carbide or aluminum oxide is added for stabilization. In addition, open-pore metallic foam structures with a pore diameter of 10 ppi to about 50 ppi can be produced by special precision casting techniques.

The carrier can in principle also be extruded and injection-molded. Again, metallic and ceramic materials are possible, in the case of ceramic materials, for example, form aids are added and, for example, binders and other additives. Extruded carriers can take any geometry, preferably those mentioned above.

The invention will now be explained in more detail with reference to some not to be understood as limiting to the scope of the invention exemplary embodiments. Exemplary embodiments:

example 1

The catalyst according to the invention is prepared according to the following procedure:

First, the water uptake of a dried zeolite was determined (H-BEA-35: commercial product of Sud-Chemie AG). It was 92.3%.

24.1 g of a Platinsulfitlosung (10.17 wt .-% Pt content) were made up to 62.3 g with distilled water. With this solution 67.55 g of the dried zeolite were impregnated in a mortar. The platinum concentration was 3.5% by weight. The moist powder was dried at 120 ⁰ C and then calcined for 5 hours at 800 ⁰ C under inert gas (V = 2 l / min) and reduced with 5% H ₂ in N ₂ for 5 h at 300 ⁰ C.

70 g of the powder was suspended in 230 ml of water using an Ultra-Turrax-Ruhrmer. The suspension was milled with a planetary ball mill (Retsch PM 100) with 10 mm spheres of yttria-stabilized Zr oxide to a particle size of d ₅₀ ~ 2 μm. With this washcoat, a codierite honeycomb (400 cpsi) was coated and calcined so that in the end 3.5 g of Pt / L honeycomb volume was contained on the honeycomb.

Example 2

To investigate the influence of the reduction, a second honeycomb was coated with a non-reduced catalyst (otherwise analogously to Ex. 1). Comparative Example 1

As a comparison, the same synthesis with ethanolammonium hexahydroxoplatinate solution (13.59 wt .-% Pt content) as Pt

Source performed. The Pt concentration was also 3.5% by weight.

Comparative Example 2:

Based on DE 10 2007 057 305 and EP 800 856 Bl, a DOC catalyst was prepared according to the following procedure:

It was first the water uptake of a mixed oxide of alumina and silica (Siralox 5/140, 5% Si, of

Condea). It was 53.86%. 110.4 g of a solution of ethanolammonium hexahydroxoplatinate (13.59% Pt content) was made up to 161.6 ml (destilled with H ₂ O). 300 g of the siralox powder were impregnated in a planetary mixer with this solution. The moist powder was oven dried at 80 ⁰ C for 3 h and then calcined at 550 ⁰ C for 3 h.

140 g of the powder was suspended in 700 ml of water using an Ultra-Turrax stirrer. The suspension is treated with a bead mill (Dynomil Fa. WAB) with 1 to 1.2 mm beads of Zr / Ce.

Oxide milled to a particle size dso ~ 3 microns. 140 g of an iron-exchanged β-zeolite (3% Fe ₂ O ₃ , β-35 zeolite) were added to this finely ground dispersion of Pt / siralox and the suspension was made up to 1400 ml, giving a coating washcoat of 20% solids content originated. A cordierite honeycomb (400 cpsi) was coated with this washcoat and calcined to finally contain 3.5 grams of Pt / 1 honeycomb volume on the honeycomb. Comparative Example 3

As a comparison of the catalytic activity and the aging, a commercially available DOC catalyst of a Daimler OM646 engine was additionally used.

Comparative Example 4

Pt / Pd (4: 1) catalyst:

First, the water uptake of a mixed oxide of alumina and silica (Siralox 5/140 Type C with very large pores and 5% Si from Condea) was determined. It was 151%. 67.39 g of a solution of ethanolammonium hexahydroxoplatinate (13.85% Pt content) was made up with 58 ml of distilled water. With this solution, 186 g of the siralox powder was impregnated in a planetary mixer in a first step. Then, 17.34 g of a palladium nitrate solution was diluted with 58 ml of water, and further added dropwise in the next step as an impregnation solution to the wet powder in the planetary mixer. The moist powder was oven dried at 80 ⁰ C for 3 h and then calcined at 550 ⁰ C for 3 h. The powder contained 7% total precious metal content.

140 g of the powder was suspended in 700 ml of water using an Ultra-Turrax-Ruhrmer. The suspension was ground with a bead mill (Dynomill Fa. WAB) with 1 - 1.2 mm Zr / Ce oxide beads to a particle size d ₅₀ ~ 3 μm. This washcoat was coated with a cordierite honeycomb (400 cpsi) and calcined to give 3.5 g at the end

Precious metal / L honeycomb volumes were contained on the honeycomb. Comparative Example 5:

Pt catalyst without zeolite:

It was first the water absorption of a mixed oxide

Alumina and silica (Siralox 5/140 Type C with very large pores and 5% Si from Condea). It was 151%. 73.6 of a solution of ethanolammonium hexahydroxoplatinate (13.59% Pt content) was made up to 181 ml with distilled water. With this slogan was in a planetary mixer

200 g of siralox powder impregnated. The moist powder was oven dried at 80 ⁰ C for 3 h and then calcined at 550 ⁰ C for 3 h.

100 g of the powder was suspended in 200 ml of water using an Ultra-Utrax-Ruhrmer. The suspension was ground with a planetary ball mill (Ra. Retsch) with 10 mm Zr oxide beads to a particle size of dso ~ 3 μm. To empty the grinding container 200 g of water were added. A cordierite honeycomb (400 cpsi) was coated with this washcoat and calcined to finally contain 3.5 grams of Pt / 1 honeycomb volume on the honeycomb.

Example 6:

Comparison test of the catalysts:

The catalyst honeycombs obtained in Examples 1 and 2 and Comparative Examples were tested in a reactor under the following conditions for the oxidation of CO, propene and NO: Space velocity: 70,000 h ¹

CO: 500 ppm

NO: 500 ppm

Propene: 500 ppm

Oxygen: 5%

Water vapor: 10%

CO ₂ : 70-90 ppm

Nitrogen: rest

The catalyst honeycomb was installed with a ceramic fiber mat in a quartz glass tube. The gas flow was before the

Catalyst heated electrically. For the test, the catalyst was operated only for 30 min under these gas conditions at 390 ⁰ C and then cooled in steps of 20 ⁰ C. Each temperature was maintained for 8 minutes and the product composition determined between 7 and 8 minutes.

Below 250 ⁰ C, the cooling was carried out in 5 ° C increments around particular the CO light-off temperature to (50% CO conversion) determined more accurately.

After this test, the catalyst was flushed with air with 10% steam at a space velocity of 5000 h ^"1, and these gas conditions at 750 ⁰ C (measured in the monolith) is heated in 2 h. Under these conditions, the catalyst 10 was aged h. Then the measurement described above was repeated.

Figure 1 shows the CO conversion of the invention and the comparative catalysts. Tab. 1 shows the light-off temperatures taken from FIG. 1 (50% conversion to CO). Table of CO light-off temperatures (50% conversion)

Example ^il - CO-LOT fresh [ ⁰ C] CO-LOT aged [ ⁰ C]

Ex. 1 196 225

Ex. 2 189 224

See Ex. 1 245 278

See Ex. 2 191 233

See Ex. 3 200 220

It can be clearly seen that the pure zeolite catalyst, which also has Pt on the surface in larger clusters, which was unavoidable by the preparation with PtEA impregnation (Comparative Example 1), is significantly worse than the catalyst according to the invention.

It can also be seen that the catalyst according to the invention with respect to the CO light-off temperatures with commercially available (cf., Ex. 3) and reproduced state-of-the-art DOC catalysts (Comp. Ex. 2), based on amorphous Al / Si mixed oxides are based as platinum carriers, both in the fresh state, as well as after aging is comparable. In addition, it can be seen from the comparison of Examples 1 and 2 that a reduction of the catalyst before the reaction is of no importance here. The test conditions of 30 min under an oxidizing gas mixture at 390 ⁰ C, such effects are canceled for the catalysts of the invention. It is thus possible to use catalysts with Pt (O) or oxidic precursor.

Figure 2 and Tab. 2 show the Nθ ₂ ~ yield of these catalysts. A high Nθ ₂ ~ yield is desirable for the passive regeneration of a DPF downstream of a DOC and, in the case of an SCR stage, of nitrogen oxide reduction downstream of this DOC. Table 2: Maximum NO ₂ yield

Example Max. N0 ₂ ~ Yield Max. Nθ2 ~ Yield [%] fresh [%] aged

Ex. 1 50 37

Ex. 2 52 33

See Example 1 32 15

See example 2 60 21

See example 3 59 16

It can be clearly seen that only the catalyst of the invention after aging with 37 and 33% Nθ ₂ ~ yield still has a relatively high activity for the oxidation of NO to NO ₂ .

Example 7:

Comparison test under sulfur aging:

As it is known that Pt / Pd catalysts are more resistant to aging, but are more sensitive to sulfur than pure ones

Platinum catalysts, a test was carried out after aging with sulfur poisoning after aging.

For this purpose, first as described in Example 6, an activity test of 390 ⁰ C carried out downward, then the aging, as described in Example 6 and then again a test after thermal aging. After that was with a

Space velocity of 5000 h ^"1, a gas mixture of 20 ppm SO ₂ in air was passed over the catalyst for 2 h at 250 ^° C. Subsequently, an activity measurement was carried out, cooling off from 390 ^° C. The catalyst was then heated at 10 ° % Water vapor at a space velocity of 5000 h ^"1 desulfurized again by heating over a period of 1 h of 150 ⁰ C to 750 ⁰ C and then 15 min at 750 ° C was held. After this high-temperature desulfurization, an activity test was again carried out, starting from 390 ^° C., as described in Example 6.

Table 3 shows the CO light-off temperatures for the different catalysts:

It can be clearly seen that the catalyst according to the invention behaves here very much like the pure platinum catalyst according to the prior art on amorphous Al / Si oxide (cf. Example 5). The Pt / Pd catalyst (See Example 4) is significantly more thermostable. The optimum Pt / Pd alloy was not formed by calcination at 550 ⁰ C in the preparation so that the catalyst in the 750 ° C aging was even better. It can also be seen that sulfur poisoning is approximately reversible both for the Pt / Pd catalyst and for the catalyst for CO oxidation according to the invention. However, the great advantage of the Pt catalyst according to the invention is shown by considering the NO oxidation. The maximum yields of NO ₂ are shown in Table 4. Table 4: NO oxidation after sulfur aging

It can be clearly seen that the catalyst according to the invention shows less thermal aging than the pure one

5), but remains unchanged after this thermal aging, regardless of the sulfur, the Pt / Pd catalyst (Cf. Example 4) is also thermally stable, but even after the drastic thermal aging, it is still by Deactivated sulfur. Especially when the catalyst is heated to high after being loaded with sulfur, it is strongly deactivated in the desulfurization process for NO oxidation. That a desulfating reaction has indeed taken place can be seen from the fact that the CO oxidation again became better (Table 3, Cf. Example 4). In this desulfurization process, however, the Pt / Pd catalyst was again significantly deactivated for NO oxidation (maximum NO ₂ yield 28%). This deactivation can not be observed in the catalyst according to the invention, but this process is very relevant in practice. If a DOC catalyst in a system with actively regenerated DPF often has to generate high temperatures for DPF regeneration by hydrocarbon combustion, this deactivation is very crucial. In the normal operating phases of the catalyst between the regenerations of the works

Catalyst always in SO ₂ -containing exhaust gas at lower temperature (0 - 500 ⁰ C). He is loaded here with SO ₂ . Any active Regeneration means a very high temperature increase in temperature and leads to the deactivation of the prior art Pt / Pd catalysts described here, but not to a deactivation of the catalyst according to the invention.

Example 8:

Determination of the Pt distribution

To determine the Pt distribution on the zeolite, an IR spectroscopic method was developed. The method is based on the comparison of the Pt-C = O stretching vibration before and after the adsorption of 1-adamantanecarbonitrile. 1-adamantanecarbonitrile is a sterically bulky molecule that, due to its size, can not penetrate into the pore system of the zeolite and therefore binds selectively to the Pt clusters on the outer surface. If one compares the amount of carbon monoxide that binds to the Pt clusters before and after the poisoning, the distribution of the Pt can be determined.

Carrying out the measurement:

From the Pt-zeolite powder, a pressure of about 20 mg was prepared. This pressure was dried before the measurement at 400 ^° C. under high vacuum (~ 10 ^{~ 7} mbar) overnight.

Before measuring the reference spectrum, 20 mbar carbon monoxide was adsorbed on the sample. Then, the first measurement of the total adsorbed amount of CO was carried out. (Integral of the CO peak). Before the poisoning, the sample was again thermally treated at 400 ⁰ C to the

Desorb carbon monoxide and thus allow poisoning with 1-adamantanecarbonitrile. For the poisoning 2.5 mbar of the nitrile were absorbed and then metered in again 20 mbar CO. After about 10 minutes, the comparison spectrum was measured.

Fxgur 3 shows the IR spectra of PSA-BEA and PtEA-Bea before and after poisoning with 1-adamantanecarbonitrile

The left spectrum shows the catalyst according to the invention, the right one the catalyst according to Comparative Example 1, prepared with ethanolammonium hexahydroxoplatinate. The erfmdungsgemaße catalyst adsorbs both in the original and in the poisoned state, approximately the same amount of carbon monoxide. This means that the platinum is not accessible to the nitrile and thus is inside the zeolite (in the pores). In contrast, the adamantane nitrile-poisoned catalyst of Comparative Example 1 adsorbs significantly less CO than the non-poisoned catalyst. This means that the Pt distribution on both zeolites is different and correlates with the activity as well as the stability of the two catalysts. It is thus clearly advantageous to introduce the platinum completely into the interior pore system of the zeolite.

The different Pt distribution is additionally confirmed by XRD measurements. The spectrum of the inventive catalyst shows no Pt reflections, whereas the spectrum of the catalyst according to Comparative Example 1 shows clear reflections.

Claims

claims A process for producing a platinum-containing zeolite comprising the steps a) impregnating a zeolite with a PlatinsulfitIosung, b) calcining the impregnated zeolite under a protective gas atmosphere. 2. The method according to claim 1, wherein the calcining takes place in an argon, helium, neon or nitrogen atmosphere. 3. The method according to claim 1 or 2, wherein the calcining takes place at a temperature of 600 to 900 ⁰ C. 4. The method according to any one of claims 1 to 3, wherein after the calcination, a reduction takes place. 5. The method of claim 4, wherein the reduction is carried out with a mixture of reducing gas and an inert gas. 6. The method according to any one of claims 4 or 5, wherein the reduction over a period of 3 to 7 hours. 7. The method according to any one of claims 4 to 6, wherein the reduction is carried out at a temperature of 200 to 500 ⁰ C. 8. The method according to any one of claims 1 to 7, wherein a zeolite is used as zeolite, selected from the Group consisting of types AEL, BEA, CHA, EUO, FAU, FER, KFI, LTA, LTL, MAZ, MOR, MEL, MTW, LEV, OFF, TONE and MFI. 9. The method according to any one of claims 1 to 8, wherein the zeolite used has a SiO ₂ ZAl ₂ O ₃ -ModUl from 5 to 300. 10. zeolite prepared by a process according to any one of claims 1 to 9. 11. zeolite containing at least 2 wt .-% platinum, characterized in that at least 90% of the platinum are in the pores of the zeolite. 12. A zeolite according to claim 10 or 11, characterized in that at least 95% of the platinum is in the pores of the zeolite. 13. A zeolite according to any one of claims 10 to 12, characterized in that the zeolite contains at least 3 wt .-% platinum. 14. A zeolite according to any one of claims 10 to 13, wherein the Zeolite selected from the group consisting of the types AEL, BEA, CHA, EUO, FAU, FER, KFI, LTA, LTL, MAZ, MOR, MEL, MTW, LEV, OFF, TON and MFI. 15. A zeolite according to any one of claims 10 to 14, wherein the zeolite has a Si0 ₂ / Al ₂ 0 ₃ modulus of 10 to 300. A zeolite according to any one of claims 10 to 15, wherein the zeolite is a metal-exchanged zeolite. 17. A zeolite according to any one of claims 10 to 16, characterized by a Pt-C = O stretching vibration between 2070 and 2110 cm ^"1 , preferably at about 2080 to 2095 cm ^{■ "■} and / or wherein the X-ray diffractogram (XRD) is free of Pt-reflections. 18. Use of a zeolite according to any one of claims 10 to 17 as an oxidation catalyst and Hydrocarbon storage. 19. Catalyst component containing a zeolite according to one of claims 10 to 17. 20. catalyst component according to claim 19 comprising a carrier, wherein the zeolite is present as a coating on the carrier.